Gravitational collision enhanced upgrading of heavy oils

ABSTRACT

The present invention relates to gravitational collision enhanced upgrading of heavy oils, It thus describes a thermodynamic cracking process for heavy oil, extra heavy oil and bituem as well as a thermodynamic cracking unit for carrying out the process.

FIELD OF THE INVENTION

The present invention is related to a process for gravitationalupgrading and hydrogenation of heavy oil, extra heavy oil, bitumen andthe like by increasing its API value, reduction of its viscosity andremoval of part of the sulphur and heavy metals in the oil.

BACKGROUND.

The following general introduction to catalytic cracking highlightspresent status and the outlined words and sentences focus on thedifficulties/precautions which have to be met from case to case.

Catalytic cracker unit (FCCU) processes are widely utilized in thepetroleum industry in the upgrading of oils. The ‘heart’ of suchprocesses consists of a reactor vessel and a regenerator vesselinterconnected to allow the transfer of spent catalyst from the reactorto the regenerator and of regenerated catalyst back to the reactor. Theoil is cracked in the reactor section by exposing it to hightemperatures and in contact with the catalyst. The heat for the oilcracking is supplied by the exothermic heat of reaction generated duringthe catalyst regeneration. This heat is transferred by the regeneratedfluid catalyst stream itself. The oil streams (feed and recycle) areintroduced into this hot catalyst stream en route to the reactor. Muchof the cracking occurs in the dispersed catalyzed phase along thistransfer line or riser.

The final contact with the catalyst bed in the reactor completes thecracking mechanism. The vaporized cracked oil from the reactor issuitably separated from entrained catalyst particles by cyclones androuted to the recovery section of the unit. Here it is fractionated byconventional means to meet the product stream requirements. The spentcatalyst is routed from the reactor to the regenerator after separationfrom the entrained oil. Air is introduced into the regenerator and thefluid bed of the catalyst. The air reacts with the carbon coating on thecatalyst to form CO/CO₂. The hot and essentially carbon-free catalystcompletes the cycle by its return to the reactor. The flue gas leavingthe regenerator is rich in CO. This stream is often routed to aspecially designed steam generator where the CO is converted to CO₂ andthe exothermic heat of reaction used for generating steam (the COboiler). The principal difference between the present invention and thisprior art, is that CO/CO₂ is not routed to any external boiler, butplays a vital part in the present invention by production of hydrogen bythe gas/water shift expressed by CO+H₂=H₂+CO₂.

Feed stocks to the FCCU are primarily in the heavy vacuum gas oil range.Typical boiling ranges are 340° (10%) to 525° C. (90%). This allowsfeedstock with final boiling point up to 900 C. This gas oil is limitedin end point by maximum tolerable metals, although the new zeolitecatalysts have demonstrated higher metal tolerance than the oldersilica-alumina catalysts.

The principal difference between present invention and this option isthat the present invention is not limited by its metal content as theprocess reduces the metal content in the order of 90%, forming metalsulphides. In addition the process does not require use of an advancedcatalyst, but use fine grain minerals, such as inter alia silicon oxideand olivine as heat carrier.

The fluid catalytic cracker is usually a licensed facility. Correlationsand methodology are therefore proprietary to the licensor althoughcertain data are divulged to clients under the licensor agreement. Suchdata are required by clients for proper operation of the unit, and maynot be divulged to third parties without the licensor's expressedpermission.

These and other means, including operating instructions, are requiredfor the proper operation of the units. Most of the proprietary data,however, concern the reactor/regenerator side of the process. Therecovery side—that is, the equipment required to produce the productstreams from the reactor effluent—utilizes essentially conventionaltechniques in their design and operating evaluation.

Up to the late 1980s feedstock to FCCU were limited by characteristicssuch as high Conradson carbon and metals. This excluded the processingof the ‘bottom of the barrel’ residues. Indeed, even the processing ofvacuum gas oil feeds were limited to

-   -   Conradson carbon<10 wt %    -   Hydrogen content>11,2 wt %    -   Metals NI+V<50 ppm

During the late 1980s significant breakthroughs in research anddevelopment produced a catalytic process that could handle these heavyfeeds and indeed some residues. Feed stocks heavier than vacuum gas oilwhen fed to a conventional FCCU tend to increase the production of cokeand this in turn deactivates the catalyst. This is mainly the result of:

-   -   A high portion of the feed that does not vaporize. The        un-vaporized portion quickly cokes on the catalyst, choking its        active area.    -   The presence of high concentrations of polar molecules such as        polycyclic aromatics and nitrogen compounds. These are absorbed        into the catalyst's active area causing instant (but temporary)        deactivation.    -   Heavy metals contamination that poisons the catalyst and affects        the selectivity of the cracking process.    -   High concentration of polynaphthenes that dealkylate slowly.

The present invention does not suffer from any of these drawbacks whichwill be highlighted later.

In the FCCU process conventional feedstock cracking temperature iscontrolled by the circulation of hot regen catalyst. With the heavierfeedstock, with an increase in Conradson carbon there will be a morepronounced coke formation. This in turn produces a high regen catalysttemperature and heat load. To maintain heat balance, catalystcirculation is reduced, leading to poor or unsatisfactory performance.Catalyst cooling or feed cooling is used to overcome this high catalystheat load and to maintain proper circulation.

In the present invention, the temperature of the energy carrier iscontrolled by internal cooling in the regenerator for steam productionwhereby a constant flow of heat carrier can be obtained.

The extended boiling range of the feed, as in the case of residues,tends to cause an uneven cracking severity. The lighter molecules in thefeed are instantly vaporized on contact with the hot catalyst andcracking occurs. In the case of the heavier molecules vaporization isnot achieved as easily. This contributes to a higher coke depositionwith a higher rate of catalyst deactivation. Ideally, the whole feedshould be instantly vaporized so that a uniform cracking mechanism cancommence. The mix temperature (which is defined as the theoreticalequilibrium temperature between the un-cracked vaporized feed and theregenerated catalyst) should be close to the feed dew point temperature.In conventional units this is about 20-30°C. above the riser outlettemperature. This can be approximated by the expression:

T _(m) =T _(R)+0,1 ΔAH _(c)

-   -   T_(m)=the mix temperature    -   T_(R)=riser outlet temperature (° C.)    -   ΔAh_(c)=heat of cracking (BTU/lb or kJ/kg)

This mix temperature is also slightly dependent on the catalysttemperature.

Cracking severity is affected by polycyclic aromatics and nitrogen. Thisis due to the fact that these compounds tend to be absorbed into thecatalyst. Raising the mix temperature by increasing the risertemperature reverses the absorption process. Unfortunately, a higherriser temperature leads to undesirable thermal cracking and productionof dry gas.

The processing of heavy feedstock therefore requires special techniquesto overcome:

-   -   Feed vaporisation.    -   High concentration of polar molecules.    -   Presence of metals.

Some of the techniques developed to meet heavy oil cracking processingare the following:

-   -   Two-stage regeneration.    -   Riser mixer design and mix temperature control (for rapid        vaporization).    -   New riser lift technology minimizing the use of steam.    -   Regen catalyst temperature control (catalyst cooling).    -   Catalyst selection for:    -   Good conversion and yield pattern.    -   Metal resistance.    -   Thermal and hydrothermal resistance.    -   High-gasoline RON.

The present invention will show how this is solved and demonstrate thatit is not needed to use two-stage regeneration.

An important issue in the case of heavy oil fluid catalytic cracking isthe handling of the high coke deposition and the protection of thecatalyst. One technique that limits the severe conditions inregeneration of the spent catalyst is a two-stage regenerator.

This differs from the present invention as we do not use classiccatalysts with rare earth minerals but neutral minerals as heat carrier.In the description of the present invention the terms “catalyst” and“heat carrier” are used interchangeably.

The spent catalyst from the reactor is delivered to the firstregenerator. Here the catalyst undergoes a mild oxidation with a limitedamount of air. Temperatures in this regenerator remain fairly low,around 700-750° C. From this first regenerator the catalyst ispneumatically conveyed to a second one. Here excess air is used tocomplete the carbon burn-off and temperatures up to 900° C. areexperienced. The regenerated catalyst leaves this second regenerator toreturn to the reactor via the riser. The technology that applies to thetwo-stage regeneration process is innovative in that it achieves theburning off of the high coke without impairing the catalyst activity. Inthe first stage the conditions encourage the combustion of most of thehydrogen associated with the coke. A significant amount of the carbon isalso burned off under mild conditions. These conditions inhibit catalystdeactivation.

The present invention operates with a temperature of 800-900 C in thelower part of the regenerator and at 450-550 C in the upper part of theregenerator, which is below the temperature presented above.

It has been found that there is a specific temperature range for theenergy carrier that is desirable for a given feed and catalyst system. Aunique dense phase energy carrier cooling system provides a techniquethrough which the best temperature and heat balance relationship can bemaintained.

These features are a vital part of the present invention.

It is reported that 69% of the enthalpy contained in the heat input tothe reactor is required just to heat and vaporize the feed. Theremainder is essentially available for conversion. To improve conversionit would be very desirable to allow more of the available heat to beused for conversion. The only variable that in conventional FCCU's unitscan be changed to achieve this requirement is the feed inlet enthalpy,that is, through preheating the feed. Doing this, however, immediatelyreduces the catalyst circulation rate to maintain heat balance. This hasan adverse effect on conversion. The preheating of the feed, however, iscompensated for by cooling the energy carrier. Thus the circulation rateof the energy carrier can be retained and, in many cases, increased.Indeed, by careful manipulation of the heat balance, the net increase inenergy carrier circulation rate can be as high as 1 unit cat/oil ratio.The higher equilibrium activity for the energy carrier possible at thelower regeneration temperature also improves the unit yield pattern.

This is an important feature of the present invention, preheating of theoil still allows a high flow of energy carrier and oil feed as thegenerated CO/CO2 and steam from the atomization of the oil, dramaticallyreduces the partial pressure of the oil whereby the oil behaves as beingevaporated under high vacuum. In addition, the gravitational acceleratedcolliding jets of energy carriers induces mechanical shear forces whichimproves the cracking, i.e. allows more of the energy to be utilized inconversion.

In residue cracking commercial experience indicates that operations atregenerated catalyst temperatures above 900° C. result in poor yields,with high gas production due to local thermal cracking of the oil oncontact. Where certain operations require high regen temperatures theinstallation of a catalyst cooler will have a substantial economicincentive. This will be due to improved yields and catalyst consumption.

This is also a feature of the present invention, as low partial pressurepermits a low temperature of the energy carrier, which either can becontrolled by an internal heat exchanger in the regenerator or byrecirculation of flue gas after the downstream system (condensers).

The equilibrium temperature between the oil feed and the regeneratedcatalyst must be reached in the shortest possible time. This is requiredin order to ensure the rapid and homogeneous vaporization of the feed.To ensure this it is necessary to design and install a proper feedinjection system. This system should ensure that any catalystback-mixing is eliminated and that all the vaporized feed components aresubject to the same cracking severity.

This is achieved in the present invention by the atomisation of the oil,the gravitationally colliding jets of heat carrier and remixing ringsinside the oil cracker.

Efficient mixing of the feed finely atomized in small droplets isachieved by contact with a pre-accelerated dilute suspension of theregen catalyst. Under these conditions feed vaporization takes placealmost instantaneously.

According to the present invention it is achieved that the low velocityof the energy carrier in the regenerator is accelerated by gravitationalforces and reduced cross section area in two collision pipes by entranceinto the oil cracker.

Another problem encountered in heavy oil cracking is the possibilitythat the heavier portion of the oil is below its dew point. To ensurethat this problem is overcome, the mix temperature must be set above thedew point of the feed. The presence of polycyclic aromatics also affectscracking severity. Increasing the mix temperature to raise the risertemperature reverses the effect of polycyclic aromatics. In so doing,however, thermal cracking occurs, which is undesirable. To solve thisproblem it is necessary to be able to independently control the risertemperature relative to mix temperature.

This problem is overcome in the present invention by the low partialpressure of the oil and the fact that the oil cracker temperature iscontrolled by the injection rate of steam in the atomizing nozzles,which is independent of the feed whereby optional cracking conditionsare obtained.

Mix temperature control (MTC) is achieved by injecting a suitableheavy-cycle oil stream into the riser above the oil feed injectionpoint. This essentially separates the riser into two reaction zones. Thefirst is between the feed injection and the cycle oil inlet. This zoneis characterized by a high mix temperature, a high catalyst-to-oil ratioand a very short contact time.

This is avoided according to the present invention since the heattransfer, vaporization and cracking takes place instantaneously in theoil cracker and is completed by the entrance of the cyclone.

As described earlier, it is highly desirable to achieve goodcatalyst/oil mixing as early and as quickly as possible in the process.The method described to achieve this requires the pre-acceleration anddilution of the catalyst stream. Traditionally, steam is the medium usedto maintain catalyst bed fluidity and movement in the riser. Steam,however, has a deleterious effect on the very hot catalyst that is metin residue cracking processes. Under these conditions steam causeshydrothermal deactivation of the catalyst.

This is overcome in the present invention by using the off gases fromthe regenerator (CO/CO2) as the main carrier of the energy carrier andthat the heat carrier is injected at a positive angle into the oilcracker whereby the heat carrier flow is turned from an almost downwarddirection to an upward direction in the oil cracker.

Much work has been done in reducing the use of steam in contact with thehot catalyst. Some of the results of this work showed that if thepartial pressure of steam is kept low, the hydrothermal effects aregreatly reduced in the case of relatively metal free catalysts. A moreimportant result of the work showed that light hydrocarbons impartfavorable conditioning effects to the freshly regenerated catalyst. Thiswas pronounced even in catalysts that were heavily contaminated withmetals.

This one of the novel features of the present invention, namely thatcommon mineral oxides may be used as energy carriers for oil with highmetal and sulphur content. Furthermore, the use of the flue gas as heatcarrier reduces the process temperature to an optimal temperature forhydrogen production by the gas/water shift.

Light hydrocarbon gases have been introduced in several heavy oilcrackers since 1985. They have operated either with lift gas alone ormixed with steam. The limitations to the use of lift gas rests in theability of downstream units to handle the additional gas.

This is also a novel feature of the present invention, namely that wecan handle the non-condensable gases in the downstream system. By usingthe off gases from the regenerator itself to carry the energy carrier,it is also possible to utilize the calorimetric heat in the gas, whichreduces the energy consumption.

The cracked products leaving the FCCU reactor represent a wide range ofcuts. This reactor effluent is often referred to as a ‘syn’-crudebecause of its wide range of boiling point materials.

The ‘syn’-crude assay should comprise at least a TBP (True BoilingPoint) curve with an analysis of light ends, gravity versus mid-boilingpoint curve and a PONA for the naphtha and sulphur content versusmid-boiling point for the ‘syn’-crude.

The present invention relates to a FCCU cracking unit which aims atreducing a number of the obstacles associated with existing FCCU-unitsand, more specifically, shows a FCCU-unit which can be built for smallscale operation at a well site whereby heavy feedstock can be processedat the source. The advantage obtained is that feedstock with severetransport properties (pumping capability) can be converted intoexcellent transport conditions or be used as a diluent oil to be blendedwith the heavy crude. This kind of blending is used widely in forexample Venezuela and Canada. A basic rule is that for every barrel ofoil extracted from the reservoir, ¾ barrel of diluent oil is needed toblend the oil into good pumpable conditions.

Designated Collicitor, the technology makes use of the thermodynamicimpact from oil droplets colliding with hot solid particles. TheCollicitor technology is enclosed in a compact reactor/regeneratorconcept that inherently includes high-temperature steam generation. Theconcept relies upon high energy dissipation through the collision of 40to 60 m/s hot solids jets at 100 to 200 kg/m³capable of breaking theviscous bridges at molecular level. The reaction enthalpy required forthermo-mechanical upgrading is provided from the regeneration of thesolids, from which residual coke is burnt off. Hydrogenation is furthersupported by high-temperature steam instantly impacted with the localtemperature peaks caused by colliding particles, thus, enhancing desiredhot spot reactions.

The solids to be used are naturally occurring mineral particles. Olivineis used as reference material owing to its tar cracking benefits.Furthermore, the Collicitor process is considered complementary tocommon extraction techniques because it (also) provides a part of theauxiliary steam required. In current operations, steam is usuallygenerated from natural gas, representing additional cost andenvironmental impacts.

By using light diluent oil which may have a market price of $ 25-30 perbarrel, the value of the oil is reduced to about $15 per barrel and thusa technology where one can produce diluent oil of heavy crude, will havea substantial economical potential.

The present process comprises the following main component:

1. A vertical regenerator with

a) An internal heat exchanger for steam production and

b) Discharge port for spent bed.

c) Fluidization nozzle.

d) Air intakes pipes.

e) Start up burner.

f) Fuel injection line.

Port for makeup of fresh heat carriers.

2. Two down wards pointing collision

3. An vertical oil cracker with

a) Internal remixing rings.

b) Oil atomization nozzle.

c) Port for re-circulating heat carrier.

4. Hopper for heat carrier make up

5. A transfer duct from the oil cracker to a cyclone.

6. A down comer from the cyclone to a loop seal having two exits.

7. A transfer line to a condensing/distillation system.

8. A gas circulation system.

9. A preheating system for the feed.

BRIEF DESCRIPTION OF THE DRAWINGS

Below the process will be described in detail by reference to theenclosed drawings, wherein:

FIG. 1 is a schematic flow diagram of the process according to theinvention;

FIG. 2 show the re-mixing elements in the combustor and the oil cracker;

FIG. 3 shows one embodiment of a cracker unit according to theinvention; and

FIG. 4 shows a cold experimental screening tool in plastic.

DETAILED DESCRIPTION

Referring to FIG. 1 the process is started by the combustion of oil orgas in a start up burner 3) located on a regenerator 1), heating theheat carrier in the regenerator 1). When the temperature in theregenerator 1) has reached about 400 C, fuel oil and air is injectedinto the regenerator 1) by the air compressor 2) and fuel injector 4).The combustion gasses transport the heat carrier into 2 verticalcollision pipes 8). The stream of combustion gasses and heat carrier isaccelerated by gravitational forces and by reduction of the internaldiameter whereby the velocity of the combustion gasses and heat carrieris increased and enters the oil cracker 9). The stream is divertedupwards in the oil cracker 9) and further via a transfer duct 13) to acyclone 14). The heat carrier and combustion gasses are separated in thecyclone 14) where the combustion gasses are routed to a condensationunit 22) via a transfer pipe 20). The heat carriers fall into a downcorner 15) and into a loop seal 16) having 2 exits. One exit line ispassed on to the oil cracker 9 to port 11) and one exit line to thecombustor 1) to port 6) whereby the configuration of the systemtransfers to a CFB (Circulating Fluidized Bed) configuration.

When the system has reached its operating temperature with a temperatureof the heat carrier and combustion gasses of 400 to 600 C at the lowerpart of the collision pipes 8), pre heated oil from the tank 17) ispumped to the atomization nozzle 10) where the oil is atomized by steaminjected into the nozzle 10).

In the cracker, the oil droplets will meet the two colliding andaccelerated streams of heat carrier and combustion gasses and becomeenergized by thermal energy from the heat carrier and combustion gassesand extreme mechanical shear forces from the colliding heat carrier andchange of momentums by the change of flow direction. In addition tomechanical shear forces from the colliding heat carrier, the collidingparticles will give rise semi plastic impacts creating countlesshotspots. The total effect of the heat carrier and combustion gassesheats, evaporates and crack the oil.

The combustion gasses which in addition to nitrogen, consists of CO andCO₂ will react with the steam from the atomization nozzle and forhydrogen according to CO+H₂=H₂+CO₂. In order to optimize the crackingand absorption of hydrogen into the oil, the internal of the oil cracker9) is lined with stepwise recirculation elements which generatesturbulence and cavitations in the stream which now consists of HC-gas,steam and CO₂ and NOx.

As the cracking process disposes of carbon on the heat carrier, the fueloil injection into the regenerator 1) is gradual reduced whereby excessair from the compressor 2) combusts the associated coke on the heatcarrier. The combustion temperature is in the range between 800 and 900C whereas the target temperature at the lower part of the collisionpipes 8) is in the range of 400-600 C, the excess heat in theregenerator 1) is reduced by cooling either with a heat exchanger 23)producing either hot water or steam or with recycling flue gas from agas blower 21) or a combination of the same.

In the cracking process, sulphur is removed from the oil as elementarysulphur and disposed of on the heat carrier together with portion of theheavy metals in the oil.

When the heat carrier is destroyed, spent bed is discharged via a conevalve 5) and into a spent bed cooler 7) where the temperature is reducedfrom regenerator temperature to about 125 C. The spent bed is replacedby fresh heat carrier from the hopper 12).

The produced oil is extracted from the condensation or distillationsystem in a conventional manner.

Because of the low partial pressure of the oil in the exhaust gases, itis possible to run the process at a temperature as low as 450 C.

To have the hydrodynamics of the technology tested, a cold experimentalscreening tool in plastic was built as shown in the FIG. 4. The rig wastested at University de Technologie, Compiegne, France showing excellenthydrodynamic behavior.

FIG. 2 shows the lay-out of the re-mixing elements in both theregenerator and the oil cracker. The elements have a cone 24) startingat a diameter of D1 at an angle of about 30 deg. which extends at adiameter D2. A vertical portion 25) which ends at 26) terminates into asharp edge where the diameter is increased to D2. When the gaseousstream flow upwards, it is accelerated over the conical part 24) of theelement and maintain its velocity over the vertical portion 25). At theend of the vertical portion 26) it expands violently at the sharp edgecausing extreme turbulence and reduced velocity over the portion withthe increased diameter D2 causing extreme collisions between the heatcarrier.

In order to balance the heat distribution between the regenerator andthe oil cracker, a portion of the heat carrier can be diverted over theloop seal 16) at a reduced temperature to the oil cracker where it willblend with the stream from the collision pipes 8) thus giving the targettemperature of the inflow up the oil cracker given by:

Q=m _(s) *c _(s) *t ₁ +m _(g) *c _(g) *t ₁=(m _(s) +m _(rs))*c _(s) *t ₂+m _(g) *c _(g) *t ₂ kJ

Where:

m_(s)=heat carrier from the regenerator, kg/h

c_(s)=specific heat for heat carrier, kJ/kgC

t₁=temperature in the collision pipes, C

m_(g)=combustion gasses from regenerator, kg

c_(g)=specific heat of combustion gasses, kJ/kgC

m_(rs)=re-circulated heat carrier into oil cracker, kg/hr

t₂=target temperature in the bottom of the oil cracker, C

This allow us to fine tune the optimal cracking conditions in the oilcracker and maintaining the mass flow of heat carrier.

A further positive effect of the process is that the re-mixing elementsreduce the risk for uncontrolled back mixing and cracking in the cyclonewhich is observed and controlled by the ext temperature at the inlet tothe cyclone. The suppression of over cracking is furthermore suppressedby the fluidization stream of steam in the down comer 15) of the cyclonewhere the steam molecules together with the non condensable gassesdilute the oil gas flow preventing the oil molecules inre-polymerization.

In the oil cracker, the energy consumption of the heavy oil can beexpressed as:

Q=m _(o)*(c _(o) *t _(p) +r _(o))=kJ/hr

Where:

m_(o)=injected oil, kg/hr

c_(o)=specific heat of heavy oil ranging from 2-4 kJ/kgC

t_(p)=process temperature C

r_(o)=heat of evaporation of oil kJ/kg ranging from 200-400 kJ/kg

C=heat of cracking ranging from 500 to 2000 kJ/kg

Note: the c_(p) is an average specific heat for all fractions in the oiland r₀=is an average heat of evaporation.

1. A thermodynamic cracking process of heavy oil, extra heavy oil andbitumen, characterized in that cracking is carried out in an reactor(oil cracker) having re-circulation rings under the influence two ormore gravitational and accelerated jets of hot mineral heat carrier andcombustion gasses, colliding jets injected at a positive angle into thelower part of the oil cracker whereby the stream will be divertedupwards introducing mechanical shear forces and hotspots which togetherwith an operating temperature between 450 C and 600 C cracks the oilinjected and atomized at the bottom of the oil cracker.
 2. Thethermodynamic process in accordance with claim 1, characterized in thatthe energy carrier is selected from fine grained minerals, such assilica, magnesium oxide, aluminum oxide, copper oxide, anorthisite,olivine or similar materials.
 3. The thermodynamic process in accordancewith claim 1, characterized in that hydrogen is produced in the oilcracker by the gas/water shift CO+H₂0═H ₂+C0₂ where the hydrogenhydrogenates the cracked oil gas in the oil cracker under the influenceof cavitations due to internal remixing rings.
 4. The thermodynamicprocess in accordance with claim 1, characterized in that the energycarrier is regenerated in a fluidized regeneration chamber havingfluidizing fluidization nozzles above a plenum receiving air and wherethe energy carrier is regenerated by oxidizing co-accumulated cokecontained therein and that the regenerator have internal recirculationrings for optimizing combustion conditions.
 5. The thermodynamic processin accordance with claim 4, characterized in that the regeneratorcomprises a heat exchanger and a recirculation pipe for flue gas tocontrol the temperature of the energy carrier in the reactor by steamgeneration in the heat exchanger.
 6. The thermodynamic process inaccordance with claim 1, characterized in that regenerated energycarrier is transported pneumatically and by gravitational fall down 2pipes termed collision pipes which at their lower ends are diverted toconnect with an oil cracker and that the internal diameter is reduced inorder to accelerate the stream of heat carrier and combustion gassesentering the oil cracker.
 7. The thermodynamic process in accordancewith claim 1, characterized in that the coke which is oxidized on theenergy carrier delivers the energy for the operation of the process andsurplus energy for steam production.
 8. The thermodynamic process inaccordance with claim 1, characterized in that the product gases arepassed to a suitable condensing system consisting of an oil- or steamcondenser or a distillation column.
 9. The thermodynamic process inaccordance with claim 1, characterized in that the feed oil is preheatedby the heat of condensation of the gases and that the oil is atomized ina an atomization nozzle by steam or gas.
 10. A thermodynamic crackingunit, characterized in that it comprises a cyclone and a down comerconnected to a loop seal with two exits whereby the heat carrier can bere-circulated either to the oil cracker or the regenerator thusoptimizing the control of the process as regard temperature and heatcarrier load.
 11. The thermodynamic cracking unit in accordance withclaim 10, characterized in that the colliding particles in the oilcracker lead to sonoluminiscense caused by the fact that gas trapped incavities on the particles and between these are exposed to adiabaticcompression whereby temperature and pressure of the gas bubbles areincreased and sonoluminescense is created by splitting of the moleculesin the gas, which can be oil gas or steam, and emits light and by thefact that part of the oxygen radicals binds to the cracked oil moleculesand thereby results in hydrogenation of the oil and that the collisionsgenerates hot spots.